Production of pure carbon dioxide



Jan. 12, 1954y W, K, LEWIS ET AL 2,665,972

PRODUCTION OF PURE CARBON DIOXIDE Filed Nov'. 13, 195o 5 sheets-sheet 1 i5 Y 0 l. u1 .vw "t (0g cg 9/ I n g/ J' 2i L JX.

Jan. l2, 1954 Y w. K. LEWIS ET AL 2,665,972

PRODUCTION OF PURE CARBON DIOXIDE Filed NOV. 13. 1950 5 Sheets-Shea?l 2 fc@ L Q 1, CO2

5 7 OXgDE HoTOJuDE Q /12 comorz di To LGlF-rff y QEGENEQATOQ A5 CO2) g 9 /1 Ccyco? QEGENEQATQQ. LIFT /4 GAS `F1G-3 Ik T I'f' CUEfr'en 74. Lewis 54m/1 Q. @um 2am Unvemofs @g Ovtorne Jan. 12, w54 w. K. I Ewls ET AL PRODUCTION OF PURE CARBON DIOXIDE 5 Sheets-Sheet 4 Filed NOV. 13. 1950 [2L/N N9. 2

FPACT/ON CD4/@BON GAS/F/ED Jan.. l2, 1954 w. K. Ll-:wls ET A1.

PRODUCTION OF' PURE CARBON DIOXIDE 5 Sheets-Sheet 5 Filed Nov. 13. 1950 l@UN 3 FPACT/O/V CARBON GA'S/F/ED F1a-(p 'B5 M W Cffff Patented Jan. 12, `1954 UNITED STATES TENT OFFICE PRGDUGTION 0F PUREl CARBON DIXEDE Warren K. Lewis, Newton, and Edwin R. Gilliland. Arlington, Mass., assign'ors to Standard Oil Development Company, a corporation vof Dela- Application November 13, 1950, Serial No. 195,262 o Claims. (Cl. 'fzegm This application is a continuation-impart of U. S. Application, Serial No. 92,812, filed May 12, '1-949.

This invention relates to the production of .pure carbon dioxide from oxidizable carbonaceous Arinaterial, and particularly to the production of carbon dioxide 'free oi inert gases, 'such as nitrogen. Mor-e particularly., the invention is concerned with the oxidation of carbonaceous material hy means of solid oxidized copper as thek Sourc of oxygen.

At present there are two chief industrial sources of carbon dioxide, namely,v as lay-products from alcohol fermentation and as recovery .from 'fiile gases. The carbon dioxide produced in the 'ormer process is pure and cheap but limited in amount. The latter source requires absorption of the CO2 in carbonate "solutions followed by boiling to release the pure gas. This operation Tis 'perfectly workable but cumbersome and "consumes very large quantities of heat. 'The amount of heat reeuired for recovery of `COs from flue gas is so 'large that it is not uncommon 'to burn extra fuel over and above that necessary to make the 'Ca A enea-p source of CO2 is, therefore, highly desirable. n y

In the production of flue gashthe oxidizing agent generally employed is air. The use of 'air introduces into the product gas large amounts of inert gases, such as nitrogen, which compliproducing pure carbon dioxide with "the aid of solid oxidizing materials possessing the necessary oxidation potential as the oxygen transfer agent under controlled reaction conditions.

It is a 'further object or this invention to provide a process for the conversion of oxidizable earoona'ceous material, particularly, linear-di- -vided `coal and coke to carbon dioxide.

A 'more specic object of this invention 'is to provide a process of the type speoiiied which will permit oxidation of the carbonaceous material by oxidized copper, without contaminating the carbon dioxide with inert gases, 'suon as nitrogen.

It is also an object of this invention 'to produce carbon dioxide `under pressure, 'thus minimizing the 'problems of compressing the carbon dioxide.

'These and other objects of the invention will *be apparent froin the description 'to follow.

Tne source of carbon trein which the carbon 'dioxide i's prepared "Ina'y be any oxidizabl'e carbonaeous material, such as chareoal, coalJ coke,

Vll)

heavy distillate oil, residual oils, gaseous hydrocarbons such as methane, natural gas, etc.. peat, shale,V oil sands, lignite, bitumen, etc. Charcoal and coke are the preferred solid starting materials, particularly coke and charcoal of low ash content. Charcoal vllines and coke breeze are particularly suitable. Methane and natural gas are the preferred gaseous raw materials. The process utilizes raw material which in other proc,- e'sse's suffer particular disadvantages.

The `solid oxygen carrier employed in place of air 4in accordance with this invention is oxidized copper by which term .is meant Cu'O, Cu2O.,-.mix 'tures of co0 and Cuao and 'the normally solid solutions o'f Cuoand Cuzo. .Depending upon the temperature employed in the oxidation reactionit may or may not be necessary to employ a carrier for the copper oxide. Carbonaceeus matelrials 'will react with oxidized copper at temperatlJS 'in the 'alge 0f 400l000 C. However, temperatures in the range of SOIL-10'00"o C. are preferred `with solid carbonaceous materials. such as coke and charcoal, While with gaseous raw materials such as inethane and natural 'gas lowe'l temperatures in 'the range of 40o-809 are pre- ',fed. At Ih'e higher tempratures., i. e. 80D- 1000 C. copper oxide sinters and therefore it is fused'with a carrier such as Alunduln, silica gel, kieselguhr, etc. When oxidizing C'ILi with oxidized copper, however, lower temperatures are satisfactory. At these lower temperatures sintering does not occur and the carrier can be dspensed with. Yet even in this instance the presence of a certain amount of inert carrier solid, e. g, sand, can assist the operator materially from a fluidization standpoint, even though the copper does not reside 'in the .grain of the solid kitself as fin Asil-ica gel. Broadly, two types of carriers can be employed; (l) materials such as lAlundum or silica whereinthe copper oxide may -become incorporated into the grain of the carrier, and (2) materials 'superlative as iiui-dizing assistants, e. g. clay, non-fused alumina powder, spent clay catalyst from 'petroleum 'oil treatment, kieselguilr, 'magnesia etc.

'The 'solid oxidized copper maybe employe-d in a finely-divided form and contacted 'with the car bonaceous raw materials either in the 'torm of a fluidized mass or a moving bed. The carbona'ceous raw materials when solid are likewise used in a linely-divided state or as a moving gravitating bed.

The vluldized state of the solid reactants anords effective contact between the soli-ds, ideal telnperature control and greatest uniformity of reactant distribution throughout the uidized mass. As a result the process is extremely flexible and may be readily controlled at the desired degree of carbon oxidation. Since the only oxygen available in the reaction zone is bound in the form of a copper oxide, the product remains free of inert gases, such as nitrogen.

In order to obtain proper luidization all solid reactants, both carbonaceous material and copper oxide, should be ground to a size that substantially all of it will pass through 1GO-mesh screen. For the best results, the ground solids should include a wide range of particle sizes, ranging upwardly from about 20 microns to about U-mesh with a large proportion of the material between about 100- and 20D-mesh.

Fluidization is accomplished in the carbon dioxide generator by means of carbon dioxide vapors produced in the reaction zone or separately introduced thereto. A portion of the CO2 product is recycled to a lower portion of the reacting solids to assure uidization over their entire height. Supercial linear ow velocities of the iiuidized gases within the iiuidized bed may vary between about 0.3 and 4 ft. per second for proper fluidization of most practical solid reactants in the particle sizes mentioned above.

Spent solid copper oxide is intermittently or continuously reoxidized with air in a separate reactor and returned stripped of air and combustion gases and fluidized in CO2 to the CO2 generation zone. The spent oxygen carrier preferably consists principally of copper contaminated with unreacted CuO and Cu20, depending upon the extent of oxidation in the CO2 generator. This mixture is conducted from the CO2 generation zone and contacted in the iluidized state with air in a combustion zone to be reoxidized principally to CuO which is thereafter returned to the CO2 generation zone. Since the reoxdation reaction in the burner is highly exothermic, all or at least a substantial part of any heat required to bring the carbonaceous material up to reaction temperature is; supplied to the carbon dioxide generator in the form of sensible heat of reoxidized copper oxide.

It has been found that carbonaceous materials will react with copper oxide at temperatures in the range of 400 C. to 1000 C., preferably '70D-1000 C. For example, CuO (on a carrier) reacts with retort coke at temperatures as low as 800 C. but preferably in the range of 80G- 950 C. for desired reaction rates. Reaction between CuO and wood charcoal is satisfactory at about '700 C., while methane reacts with CuO alone or supported on silica gel or Alundum, etc. at temperatures as low. as 400 C. Successful production of CO2 has been achieved by reacting methane with CuO (without a carrier) at temperatures in the range of 600 C. to 850 C. but an upper limit of 800 C. is preferred for this system. One can operate at temperatures below 600 C. but reaction rates fall oli appreciably. In

all instances the upper temperature limit to be employed is governed by the sintering temperature of the copper oxide. For this reason ternperatures above about 1000 C. are to be guarded against if not avoided altogether.

The reaction may be carried out in a two-vessel or three-vessel system employing fiuidized solids, or the reaction may take place in a moving-bed or soaker-type reactor.

`The reoxidation of the spent copper oxide may be carried out, while avoiding sinterine, at

4 temperatures in the range of the reaction temperatures, i. e., not above about 1000 C.

In order to assure high reaction rates and to carry carbon oxidation in the CO2 generator as far as possible, it is preferable to employ a substantial stoichiometrical excess of copper oxide over the oxidizable carbon present. Even if there should be unconverted carbon in the generator, the production of carbon monoxide therefrom will be negligible. Any carbon monoxide formed reacts rapidly with copper oxide to produce CO2, but the carbon reacts only slowly with the CO2 thus produced at the temperature in the generator. In other words, the carbon will not react rapidly enough with the CO2 produced to form CO in serious amounts.

The nature of the present invention will appear more clearly from the following detailed description of the accompanying drawings in which each ligure is a front elevation in diagrammatic form of one type of plant apparatus suitable for the practice thereof.

Figure l represents a ltwo-vessel system employing fluidized solids. The system is adaptable to any form of carbonaceous material.

Figure 2 represents the moving-bed or soakertype reactor employed with solid carbonaceous materials.

Figure 3 represents a system employing alternate moving beds of solid carbonaceous material and copper oxide.

Referring to Figure l, numeral I represents a carbon dioxide generator into which finelydivided carbonaceous material, such as coke, is led from hopper Z via line 3. To aid in the ilow of the carbonaceous material into vessel I a small amount of an aerating gas, such as carbon dioxide, may be added through line 4. Numeral 5 represents a hopper containing finely-divided solid copper oxide. The finely-divided oxide enters an upper portion of oxidation zone l via line 5. In initiating the process hot combustion gases from an auxiliary source (not shown) are introduced into vessels 'I and I and then, while continuing the now of hot gases, copper oxide is added to vessel 'I until the vessel is properly charged and the oxide heated. The hot oxide collects in withdrawal well 24 and is withdrawn from vessel 'I and passed under the pseudohydrostatic pressure in a uidized condition via line 9 into generator I, preferably at an upper level. In generator I a temperature of 800 C.

.to 1000 C., preferably 900 C. to 950 C., is maintained. When feed of coke through line 3 is initiated, reaction occurs between the coke and copper oxide forming CO2 at the prevailing reaction temperature.

The ratio of the rate at which carbonaceous feed should be fed to vessel I relative to the rate of feed of copper oxide to the same vessel is determined primarily by the chemical reactivity of the carbonaceous material. Thus, if one uses ordinary retort coke as the feed through line 3, in order to get satisfactory capacity of CO2 production from reactor I, the coke must be fed in large stoichiometric excess over the oxygen available in the entering copper oxide. This does not mean that all the oxygen of the copper oxide will be consumed in vessel I. The rate of flow of the coke, relative to the oxide, must be controlled so that there is unreduced copper oxide in the solids leaving through line I1. Along with this oxide, however, will be found a considerable amount of unreacted coke. This coke will be consumed in vessel 1, markedly increasing heat generated aceaora lemployed is, a highly active wood .charcoal `or a 'material rsuch as methane. in order to .maintain at least Va small amount of Vresidual copper oxide in the eiuent solids from. I, the ratio of carbonaceous feed to oxygen in the oxide willbe far lower than in the case of coke and, particularly the case of a material such as methane, which will be 'introduced at the Abottom of I, it `will be less than the stoichiometric amount.

In operating, using finely-divided coke as the oarbonaceous material and CuO on silica gel as Ithe oxidizing agent, generator I contains above grid 35 a fluidized mass consisting substantially of CuO introduced via line 9 at a point above the uppermost tray 43 and overflowing through ovorow weirs 44 to the lower trays -43. -The oxide has a particle size generally of 100 t0 200 mesh. The temperature of the oxide inf-the generator held at about 800 C. to 1000@ C. Temperature control of the exothermic reaction occurring in the generator I is effected in one alternative 'by means of a cooling medium circulating in the cooling coils 33 located on one or Ymore plates of the vessel I.

The generator unit is best started up, as previously related, by introduction into the bottom thereof of hot combustion gases for both iiuidn ization and heat supply. When Ithe temperature is brought up suiliciently so that active interaction of the coke and copper oxide will set in, re cycle of cooled top gas from vessel i to the vbottom of the vessel for iluidization is started and coke introduced. This soon purges gases other than CO2 from the unit. However, external CO2 may, if desired, be introduced to expedite this purging and fluidizaton. In order that the carbon contained in the coke be substantially completely converted to .CO2 a staged system is provided. For this purpose generator l contains trays, bubble plates, or other staging device 43 provided with overflow levels or downcomers 44 at intervals throughout. the vessel. The number of trays, etc. may be varied according to the production capacity desired of the vessel and the extent of the oxidation required. Although stag-ing has. been illustrated by the use of trays and downe comers, any manner of minimizing the mixing of solids entering and leaving the generator may be employed. The iiuidized materials entering the generator through lines 3 and 9 build up on the tray until the level of the overovc is reached, after which the u'dized materials pass down-l wardly in succession to thev next lower level` 'The depth of the bed on each tray is, preferably about 2 to 3 feet. .Ii'he ow of fluidiaed materials oc.- curs countercur-rent yto the upward HOW ,of fluidizing eas entering the vessel through line iii.. However, the flow rate o f the sae is. controlled so as not .to interfere with the overall downward fOW 0f the hidized .Solids- Substantiaily hure CO2 amounting to as Innen as 0.a mol. per atom of carbon in the @che charged and containing Suspended solids is with.- drawn overhead from generator I, passed through cyclone lo, and recovered through line Il. slibstantially free of entrained solids. The recovered gas is further Worked up by compression and/or absorption by conventional means not .shown- Solids separated in cyclone IQ may be returned to the uidized mass through pipe I2. Particles of vndesirahiy Small Size or excess may be diacarded throughv .line I3.

Part of the CO2 produced is removed from line II via line I4 and. introduced after cooling into the bottom of generator I, with the aid of blower 4.5 .to .mamtain filnidized v.coralitions throughout the fsoliosin .the generator, .Purge lines I5 and I6 equipped .with valves are provided vto intro dile@ Purge '.ga, .Such as CO2 into line 9, freeing the 5011;). phase flowing therethrough of excess air and vcombustion gases. The energy required tO'llft the purged Solid into vessel I -is supplied by means .0i .EQ2 introduced via line 25.

The .Spent 4Solids yC!Qi'itailficd in vessel I are removed at a rate which will secure the oxidation QI 'the Coke to CO2 `in'vessel I to the proper point. They are .then passed under the pseudo-hydro- .taiiic pressure of the huidized mass through Withdrawal Well and standpipe I 'I with the as'- sietane oi. dilution air entering through Vline I8 and carried into an `upper portion of regenerator ,1 via line 19. Additional aerating gas may be supplied through lines 32 and 34. Standpipe I may be enlarged in area so as to serve as a soa-ker in order to more completely remove carbon from the Withdrawn solids. The solid material thus removed ycontains reacted copper oxide in the form of Cu, C1120 and also some unconverted CuO, carbon, and ash, The amount of carbon 5 carried out through line I1 into regenerator "I depends upon the reactivity of Athe carbon toe ward copper oxide, which depends largely yupon the character of the carbonaceous material. However, the amount of carbon leaving generator I is preferably low, for example, about 0.1 to .about 1 Weight percent of the uidized copper oxide recycled to the regenerator. By and large, the more carbon `put through generator I, other operating conditions unchanged, the more CO2 is produced; however, the more carbon must be burned in regenerator 1. Where the demand for pure C62 is equivalent to only a limited fraction of the carbon in the fuel which .must be burnt to get heat required for other processes, as in a boiler plant, running high carbon content in generator I can be very advantageous. Thus, even using `a highly inert retort coke of low reactivity, by carrying about 3% of carbon in the oxide leaving generator I, one can produce over a third or a ton of pure CO2 per day per square foot of cross section in that unit with a net bed depth in it of 40 feet, at atmospheric pressure and an operating temperature of l000 C. Even with no staging in vessel I, about 25% of the carbon in the fuel is obtained in the form of pure CGz from generator I, the rest being used for heat produc.- tion in 5. The heat is recovered in coil i, which functions best as the water tubes of a boil,- er, With more reactive carbcns one can operate generator I at lower temperatures, secure larger productions of CO2 from it, reduce its height, recover in! higher vfractions of the total carbon of the fuel as Dure CO2, iom vessel I, or comb-ine these advantages as seems most desirable under @Illy SPQQIQ 5.912 Q QlQllmStllCeS- High ash content .oarhonaoeous :material causes rapid build up of ash .in the connor oxide to he recycled .and this ash build un not desirable. This aan may he removed, e. e., by conventional y gas clutriation equipment, applied to material` Withdrawn continuously from line ze or by insertion of the separating equipment in line 2c.

either case the recovered cooper oxide ie returned to the syst-ero through feed mechanism 5.

nantly through line 2| and the spent copper oxide becomes reoxidized predominantly to CuO. A temperature of 800 C. to 100 C. is maintained in regenerator 'I and the reaction proceeds according to the equation: 2Cu2O+OzelCuO- The superficial linear gas velocity within regenerator 1 is preferably maintained at about 0.5 to 3.0 it. per second to establish an apparent bed density up to about 70 to 80 lbs. per cubic it. for unsupported metal oxide and a bed height between grid 22 and level 23 of about 5 to 15 ft.

The reoxidized copper oxide is withdrawn under the pseudo-hydrostatic pressure of the nuidized mass via withdrawal well and standpipe 212i, and returned to generator l via line el entering near the top thereof. Aerating lines I5, It, and lift line 25 equipped with Valves are provided for introduction of purge and iiuidizing gas respectively such as CO2 or steam to strip and lift the solid phase to vessel I Where the cycle is repeated. Carbon dioxide introduced through lines I5 and IS serves to purge the uid of any remaining traces of nitrogen and air which may be, con-.- tained therein, as it is desirable to keep all but traces of nitrogen from generator I. Het spent gases containing excess air, nitrogen, etc. are removed from regenerator 'I via line 2i? and are withdrawn from the system and sent to waste heat recovery. y

The maximum temperature which can be employed anywhere in the system is that set by the tendency of the recycling solids to sinter. This is inuenced by the impurities, e. g., the composition of the ash of the fuel actually used. Consequently, this maximum allowable temperature must be determined for the case in hand. Once it is so determined, the operation must be controlled to keep within this limit. Thus, the combustion in vessel I generates a large quantity of heat. The temperature in that vessel must be kept down by controlling operation of cooling coil 25, or preferably by controlling solid circulation rate through solid cooler 39. In the latter case a portion of hot `solids is withdrawn from vessel 'I via withdrawal well and standpipe 33 and conveyed with the assistance of lift gasy preferably air entering through pipe 38, through solid cooler 39 operating as a waste heat boiler. The cooled solids are returned to vessel 'I through line Lit. I-Ieat is also evolved in vessel l. Its temperature may be controlled by coils 33, but, alternatively, if vessel i is operated at a temperature somewhat below that at the outlet of vessel I and sufficient solids be recycled through the system, the use of coil 33 may be dispensed with. It is within the scope of this invention to add to the copper oxide entering generator I a small amount of other solid materials such as alkaline carbonates and oxides which catalyze the reaction in generator I. Even inert solid heat carriers may be added.

Withdrawal wells and standpipes Il and 24 in vessels I and I respectively are located as far as possible from the end 'of the standp'ipes supplying the charges to the respective vessels. Vessels I and 'I are provided with cyclone separators I@ and 21 for removal of nely-d-iv-ided material from the outgoing gases, such as copper oxide or carbon iines and ash. The cyclone separators are equipped with dip legs I2 and 28 respectively for return of solids to the dense bed. Materials which are too small in size to remain uidized are withdrawn via lines i3 and 29 respectively. This material will also contain some ash produced in the system. Any fly4 ash not retained by the separators can be removed from the gas streams leaving the Vessels through lines il and 28 respectively by suitable means, such ,as scrubbing, if desired.

The uidized solids in vessels I and 'I are maintained at an apparent density which may go up to 70 to 80 lbs. per cubic ft. When a carrier is employed With the copper oxide the apparent density approaches the lower value.

Once the process is in operation the only additional copper oxide required is make-up material to supplant that which becomes too ne to iiuidize or which is lost by dilution with ash. The system described may be operated at atmospheric or superatmospheric pressure. It is preferred to operate the generator under superatmospheric pressure and the regenerator under atmospheric pressure.

The apparatus described in Figure 1 is also ideally suited for the conversion of gaseous and gasifiable hydrocarbons to CO2. Such hydrocarbons, e. g., methane, may be introduced into vessel I via line 3S controlled by valve 3. The hydrocarbon gas passes upwardly through grid 35 and contacts the copper oxide. In this case counter- :dow of solids and gas in vessel I, though still desirable, is unnecessary and bed depth in generator .i can be as low as a few feet. However, it is very desirable to maintain a considerable excess flow of CuO through vessel I relative to the (3l-I4 fed to assure the presence of CuO throughout the bed and in the solids eiiluent from it. At the temperature of the copper oxide the hydrocarbon reacts with it to produce CO2 and H2O which emerge from vessel I via line Ii. The water is removed from the CO2 by conventional means not shown.

Solids circulation between vessels I and 'I may also be accomplished by arranging the vessels at diiferent levels and using standpipes and dilute solids in gas suspensions to accomplish downward and upward ow respectively in a manner known in the art of iiuid solids handling.

It will be understood that the gases used for iiuidizing the various solids in transfer lines and for 'purging purposes, should be selected so as not to interfere with the reactions intended, for example, air may be employed as a fluidizing means supplied in lines i8, 32 and 35. I-Iowever, carbon dioxide, steam, CO, H2, water gas or methane is used as the fiuidizing gas in lines i5, i5, 25 and 3l. These gases consist solely of the elements carbon, hydrogen, and oxygen and are all converted under the reaction conditions in generator I to CO2 and/or water vapor. Air or nitrogen isnot to be used as the Iiuidizing gas at the latter points since it is not desirable to contaminate the CO2 product with nitrogen.

While a tWo or more vessel system of the type illustrated is essential for a continuous production of CO2, it is noted that intermittent operation carried out in a single vessel in a make and blow manner is likewise within the scope or the present invention. In this case the make AVperiod will be operated substantially at the conditions outlined above for generator i and the blow period at those conditions outlined for regenerator 'I as will be readily understood by those skilled in the art.

Figure 2 represents a diagrammatic sketch of apparatus employed in carrying out the process with the soalrer-type or moving bed reactor.

Referring to Figure 2, numeral I represents a reaction vessel to the upper end of which are added carbonaceous solid via line 2 and hot copper oxide, e. g. CuO, via line 3. It is also possible to mix the two solids before introduction into vessel I.

.asesora The solids are allowed to nl! the vessel und there,- after flow through the vessel at e predetermined rate controiled bythe .operation of valve 9- The Solids undergo reaction during passage downvvurdlt7 in the vessel I according to the equation: C-l-lCuOeCOz-l-Zcugo. The Q02 generated passes up through the solids and is removed via line 4. 1n Vessel I the solids settle at a predetermined rate Without turbulence or with only a minimum amount of turbulence To assure Cornplete conversion of carbon provision is made for the introduction of small amounts of CO2 gas into the bottom of the reaction vessel from 'line 4 via line 1 and pump 8, The reduced copper oxide is removed from vessel via line 5 at a predetermined rate and is conveyed to a regenerator not shown by the assistance of aerating gas such as air introduced via line 6. The regenera tion operation and vreturn of Ireoxidized solids to line 3 is the same as that described -in connection with Figure 1 Figure 3 represents vthe aiternate bed type of reactor. I n Figure 3 alternate beds of copper oxide contained in oxide chambers l are superimposed upon beds of carbonaceous solids such as charcoal contained in carbon chambers 2, etc. In initiating the process .each of the oxide chambers Li is lled with hot copper oxide entering the uppermost ,chamber vie .line 5 and passing vie line il to the nextglovverinost chamber.' ein. 'Similarly the solid carbonaceous material enters uppermost carbon chamber 2 ,via line Band proceeds to flow downwardly via `line until each of the carbon chambers contains the desired level of carbonaoeous material,- When ine prQCeSS .has been initiated copper oxide and carbonaceous solid .are fed to 4the respective chambers at a uniform rate determined by the rate of Withdrawal of the solids Vfrom rthe lowermost car-bon and oxide chambers respectively. In starting up the process CO; is produced in the lowermost oxide chamber, e. Ag. by passing a mixture of CO and CO2 v ia yline 3 intothelowermost ox-ide chamber l. Or, charcoal may be reacted with an excess of copper oxide in the'lowermost oxide chamber. The gases p ass upwardly through the oxide bed during which passage the CO is converted substantially to CO2. The CO2 stream vis taken off the oxide chamber v aaline 4 and is introduced into the bottom of theloyvermost carbon chamber 2. The CO2 passes upwardly through the bed of car-bonaceous material and is reduced to a mixture of CO and CQ; bythe reaction:

This mixture of CO andCQzis Withdrawn via line 1 2 and is introduced into -the `bottom ofthe next lowermost oxide chamber .whereby-the cycle is repeated. As many pairs of alternate beds may be employed Aas desired. Ihe final CO2 product is withdrawn via line! `oyerrheadtrom the uppermost oxide bed thus assuring the absence of CO in the nal product. Spentcopper `oxide is .Withdrawn from lowermost -oxide chamber via line V9 and sent to a regenerator as described.inconned tion with Figure l. The hot regenerated copper oxide is re-introduced into the reaction system via line 5. A continuous supply of carbonaceous material is furnished to the system via line 6. Any unreacted carbon from the lowermost carbon chamber is withdrawn via line I5 and returned via line l0 to supply line 6. Ash build-up is prevented by periodic withdrawal of part of the carbon via line I3. In the system described in Figure mixing or the `courier oxide and solid carbon is entirely prevented. 4'"

The V initial gaseous mixture of CO and CO2 fed to the reaction system 4obtained by oxidizing carbonaceous material with Opper oxide. nce the reaction is under way Dart of the C-O and CO2 mixture leaving one of the carbon chambers may be bled off and introduced into the"'l'vv ermost oxide chamber, e. g. via linelif The invention Will be illustrated by the following examples in which coke was reacted With Cu() deposited Aon a silica gel carrier in a system fluidized by CO2.

Run No. 1

[IemperatureTBOo O. to 906 C.; pressure in generatorll atm.

., Average f CO2, Orl-G0, T91?? m" percent percent 0. 888z|z3 1.2 2.5 880;\:4 98.' 36 0. 31' 4.5 .98.39 v0.29 6.5- 878;|;7 98. 37 0. 335 10.0 ssvis 98.43 0. so 13.5 891:!:4 98.49 0. 26 18.0 900;!:5 .98. 68 i0. 095 22.0 902:!:4 98. 57 0. 16 25.0 -903it2 .98. 55 .0. 1 4 32.5. 907i? Y98. 22 n.415 37.5. 897:1:2 97. 69 0. 91 897.-.t2 97. 07 J.. 42

Run No. 2

[Temperature- 950 C to 965" C.; pressure in generator: 1.095 atm (aver.);.superiic1a1 velocity: 0.775 ft./sec.]

- Average .0.02, per- Orl-,CO Tlv-111e .(111912) temp., P C.' cent percent 0.o A957 1 o. f

0.5 .in 0l 0 0" 1.0.-.. 9.4.4v '4..65 2.0. 98. 3 0. 810 4.0. 99. 0 0. 133 5.5. 98. 9 j 0. 230 8.0.. 954:1:2 99. 0 0. 150 11.0 99. 0 O. 104 18.5 956:1:0 98. 3 0.`81 1 21.5 955;!:2 99. 0 0. 101 24.5 99. 0 O. 180 30.0 959:1:2 99. 0 0. 122 34.0--- v99. 0 0. 129 39.0-.. 53i1 99. 0 0. 169 46.5... .99.` 0 l0.122 54.5- 961;!:1 99. 0 0. 130 61.5- 98. 8 0. 424 70.1 7 98. 7 0. 479 75.75 98. 1 l1.03 82.8. 98. 0 1. 18 88.3- 97.5 1. 67 93.17.. 97. 2 2.01 10025.... 96. 8` 2. 38 1133-.--- .96. 4 2. se

Run No. 3

[Temperature-835 C. to 850 C.; pressure in generator: 1.095 atm.

' (aver); superficial velocity: 0.5251 ft./se

Average CO2, pere TID-1e (mm') temp., ,C. cent p eeIit 3.0 3.5 835:1:0 2 5.5 837:!:0 0. 050 7.5 834i1 0(2 17 12. 50.11-78 18. (1,095 2G. y0. 205 34. 0. 095 41 0. 143 48 0. 085 gg 0. 152 sie 68. 9B. 49 0 220 77. 98. 08 0. 620 88. l 96 97 1. 71

. 11 These are batch runs, data of which are more informative as to the characteristics o the reactions. The weight percent copper, expressed as metal, in the impregnated gel at the start of the runs was 12.2 The bed densities were about 21 pounds per cubic foot, on account of the nature `of the carrier. The initial charges are shown in the following table.

Lbs. avail- Lbs. carbon able oxygen per cu. ft bed Per c- It. bed

Run No` l l. 52 0. 422 Run No. 2 0. 392 0. 578 Run No. 3 3. 32 0. 558

The net CO2 synthesis rates for Runs 1, 2, and 3 are shown respectively in Figures 4, 5, and 6. The

-high initial rates, which, however, fall on rapidly, .are believed to be due to .the fact that copper Aoxides high in oxygen (down to an atomic ratio No. 2), the net production rate of CO2 was 2.87

cu. ft. (measured at standard conditions) per hour per cu. ft. or bed. This iig'ure was low because of the low reactivity of the coke used. Carbons such as charcoal, of high reactivity, will give many fold this rate of CO2 synthesis under conditions otherwise the same.

While the foregoing description and exemplary operations have served Yto illustrate specific applications and results of the invention, Vother modifications obvious to those skilled in the art are within the scope of the invention. Only such limitations should beimposed on the invention as are indicated in the appended claims.

What is claimed is:

l. A process for producing substantially pure CO2 which comprises contacting a carbonaceous material in a reaction zone with nely divided solid copper oxide, maintaining the copper oxide inja uniform dense, turbulent iiuidized state by means of CO2 separately injected into the reaction zone, maintaining a temperature of 400 to 1000 C. in the reaction zone whereby reaction occurs between the carbonaceous material and the copper oxide to produce CO2 and a reduced copper oxide, removing a gaseous stream of substantially pure CO2 from the reaction Zone, separately withdrawing a solids stream of reduced copper oxide from the reaction zone, reoxidizing the withdrawn reduced copper oxide in a separate oxidation zone by combustion with air, coolingthe reoxidized copper oxide, purging the reoxidized copper oxide of air and gaseous combustion products by means of CO2 gas and returning the reoxidized oxide fluidized in CO2 to the reaction zone.

2. A process according to claim 1 in which the 12 carbonaceous material is a nely divided solid and in which the reaction temperature is maintained in the range of 800 C. to l000 C.

3. A process according to claim 1 in which the carbonaceous material is a gaseous hydrocarbon and in which the reaction temperature is maintained in the range of 60G-800 C.

4. A process according to claim 1 in which the copper oxide is deposited on an inert solid carrier.

5. A process for the production of substantially pure CO2 which comprises contacting finely divided coke in a reaction zone with nely divided solid copper oxide deposited on silica gel, maintaining the coke and oxide in a dense, turbulent, luidized state in the reaction zone by means of CO2 gas separately introduced thereto, maintaining a temperaturdof 800 to 1000 C. in the reaction zone whereby the coke is oxidized to CO2 and the copper oxide is reduced, removing a gaseous stream of substantially pure CO2 from the reaction zone, separately removing a solids stream of reduced copper oxide from the reaction zone, reoxidizing the reduced oxide in a separate oxidation zone by combustion with air, cooling the reoxidized copper oxide, purging the reoxidized copper oxide of air and gaseous combustion products by means of CO2 gas, and returning the reoxidized copper oxide to the reaction zone luidized in CO2.

6. A process for the production of substantially pure CO2 which comprises contacting methane in a reaction zone with finely divided solid copper oxide deposited on silica gel, maintaining the methane and oxide in a dense, turbulent, uidized state in the reaction zone by means of CO2 gas separately introduced thereto, maintaining a temperature of 400 to 800 C. in the reaction zone whereby the methane is oxidized to CO2 and the copper oxide is reduced, removing a gaseous stream of substantially pure CO2 from the reaction zone, separately removing a solids stream of reduced copper oxide from the reaction zone, reoxidizing the reduced oxide in a separate oxidation zone by combustion with air, cooling the reoxidized copper oxide, purging the reoxidized copper oxide of air and gaseous combustion products by means of CO2 gas and returning the reoxidized copper oxide to the reaction zone fluidized in CO2.

WARREN K. LEWIS. EDWIN R. GILLILAND.

References Cited in the file of this patent FOREIGN PATENTS Number Country Date 936 Great Britain 1862 10,759 Great Britain 1887 12,155 Great Britain 1892` 6,835 Great Britain 1896 587,774y Great Britain May 6, 1947 597,221 Great Britain Jan. 2l, 1948 OTHER REFERENCES Improved Solids-Gas Contacting by Fluidization, by J. C. Kalbach, June 1944 Chem. and Met. Eng., pages 94-97. 

1. A PROCESS FOR PRODUCING SUBSTANTIALLY PURE CO2 WHICH COMPRISES CONTACTING A CARBONACEOUS MATERIAL IN A REACTION ZONE WITH FINELY DIVIDED SOLID COPPER OXIDE, MAINTAINING THE COPPER OXIDE IN A UNIFORM DENSE, TURBULENT FLUIDIZED STATE BY MEANS OF A CO2 SEPARATELY INJECTED INTO THE REACTION ZONE, MAINTAINING A TEMPERATURE OF 400 TO 1000* C. IN THE REACTION ZONE WHEREBY REACTION OCCURS BETWEEN THE CARBONACEOUS MATERIAL AND THE COPPER OXIDE TO PRODUCE CO2 AND A REDUCED COPPER OXIDE, REMOVING A GASEOUS STREAM OF SUBSTANTIALLY PURE CO2 FROM THE REACTION ZONE, SEPARATELY WITHDRAWING A SOLIDS STREAM OF REDUCED COPPER OXIDE FROM THE REACTION ZONE, REOXIDIZING THE WITHDRAWN REDUCED COPPER OXIDE IN A SEPARATE OXIDATION ZONE BY COMBUSTION WITH AIR, COOLING THE REOXIDIZED COPPER OXIDE, PURGING THE REOXIDIZED COPPER OXIDE OF AIR AND GASEOUS COMBUSTION PRODUCTS BY MEANS OF CO2 GAS AND RETURNING THE REOXIDIZED OXIDE FLUIDIZED IN CO2 TO THE REACTION ZONE. 